Ethylene interpolymerizations

Abstract: Processes for polymerizing ethylene/a-olefin interpolymer compositions are disclosed. The interpolymer compositions have a controlled composition and a controlled molecular weight distribution. The processes utilize a highly-efficient homogeneous catalyst composition in at least one reactor to produce a first interpolymer having a narrow composition distribution and a narrow molecular weight distribution, and a highly-efficient heterogeneous Ziegler catalyst in at least one other reactor. The reactors can be operated sequentially or separately, depending upon the desired product. The novel compositions have good optical properties (e.g., clarity and haze) and good physical properties (e.g., modulus, yield strength, toughness and tear). Useful products which can be formed from these compositions include film, molded articles and fiber.

Description: This invention relates to ethylene interpolymers and interpolymerization processes. The processes utilize at least one homogeneous polymerization catalyst and at least one heterogeneous polymerization catalyst in separate reactors connected in series or in parallel. Interpolymers produced from such processes are thermoplastic and have surprisingly beneficial properties, including improved impact and tear properties, high modulus and higher crystallization temperatures, and are useful in making molded or shaped articles, and film. There are known several polymerization processes for producing polyethylene and ethylene interpolymers, including suspension, gas-phase and solution processes. Of these, the solution process is of commercial significance due to the advantages described in U.S. Pat. 4,330,646 (Sakurai et al.). A most advantageous solution process would be found if the temperature of the polymerization solution could be increased and the properties of the polymers suitably controlled. U.S. Pat No. 4,314,912 (Lowery et al.) describes a Ziegler-type catalyst suitable for use in high temperature solution polymerization processes. U.S. Pat No. 4,612,300 (Coleman, III) and USP 4,330,646 describe a catalyst and solution polymerization process for producing polyethylenes having a narrow molecular weight distribution. USP 4,330,646 also describes a process for producing polyethylenes with a broader molecular weight distribution in a solution process. These processes are based on heterogeneous Ziegler type catalysts which produce interpolymers with broad composition distributions regardless of their molecular weight distribution. Such ethylene polymers have deficiencies in some properties, for instance, poor transparency and poor anti-blocking properties. WO-A-87/03612 discloses the preparation of interpolymers using transition metal catalysts. Solution polymerization processes for producing ethylene interpolymers with narrow composition distributions are also known. U.S. Pat No. 4,668,752 (Tominari et al.) describes the production of heterogeneous ethylene copolymers with characteristics which include a narrower composition distribution than conventional heterogeneous copolymers. The utility of such polymer compositions in improving mechanical, optical and other important properties of formed or molded objects is also described. The complex structures of the copolymers necessary to achieve such advantages are finely and difficultly controlled by nuances of catalyst composition and preparation; any drift in which would cause a significant loss in the desired properties. U.S. Pat No. 3,645,992 (Elston) describes the preparation of homogeneous polymers and interpolymers of ethylene in a solution process operated at temperatures of less than 100°C. These polymers exhibit a "narrow composition distribution", a term defined by a comonomer distribution that within a given polymer molecule and between substantially all molecules of the copolymer is the same. The advantages of such copolymers in improving optical and mechanical properties of objects formed from them is described. These copolymers, however, have relatively low melting points and poor thermal resistance. U.S. Pat No. 4,701,432 (Welborn, Jr.) describes a catalyst composition for the production of ethylene polymers having a varied range of composition distributions and/or molecular weight distributions. Such compositions contain a metallocene and a non-metallocene transition metal compound supported catalyst and an aluminoxane. U.S. Pat No. 4,659,685 (Coleman, III et al.) describes catalysts which are composed of two supported catalysts (one a metallocene complex supported catalyst and the second a non-metallocene transition metal compound supported catalyst) and an aluminoxane. The disadvantages of such catalysts in the commercial manufacture of ethylene polymers are primarily twofold. Although, the choice of the metallocene and a non-metallocene transition metal compounds and their ratio would lead to polymers of controlled molecular structure, the broad range of ethylene polymer structures required to meet all the commercial demands of this polymer family would require a plethora of catalyst compositions and formulations. In particular, the catalyst compositions containing aluminoxanes (which are generally required in high amounts with respect to the transition metal) are unsuitable for higher temperature solution processes as such amount of the aluminum compounds result in low catalyst efficiencies and yield ethylene polymers with low molecular weights and broad molecular weight distributions. It would be desirable to provide an economical solution process which would provide ethylene interpolymers with controlled composition and molecular weight distributions. It would be additionally desirable to provide a process for preparing such interpolymers with reduced complexity and greater flexibility in producing a full range of interpolymer compositions in a controllable fashion. It would be particularly desirable to economically produce ethylene interpolymer compositions having improved impact and tear properties, improved optical properties, high modulus and higher thermal stabilities. We have now discovered polymerization processes for preparing interpolymer compositions of controlled composition and molecular weight distributions. The processes utilize at least one homogeneous polymerization catalyst and at least one heterogeneous polymerization. catalyst in separate reactors connected in series or in parallel. In accordance with the invention, there is provided a process for preparing an ethylene/α-olefin interpolymer composition, characterized by: (A) reacting by contacting ethylene and at least one other α-olefin under slurry or gas phase polymerization conditions in the presence of a homogeneous catalyst composition in at least one reactor to produce a first interpolymer which has a narrow composition distribution, (i.e., one which has a composition distribution branch index (CDBI) of greater than 50 percent where CDBI is defined at the weight percentage of polymer molecules having a comonomer content within 50 percent of the median total comonomer content as measured by the TREF technique defined herein), and a narrow molecular weight distribution (i.e. a molecular weight distribution such that Mw/Mn is less than 3), wherein 15% or less of the first interpolymer has a degree cf branching of less than or equal to 2 methyls/1000 carbons and is lacking a measurable homopolymer fraction as measured by the TREF technique, and wherein the homogeneous catalyst composition contains either no aluminum cocatalyst or contains an amount of aluminum cocatalyst which will give rise to a detectable aluminum residue in the product of less than or equal to 250 ppm, (B) reacting by contacting ethylene and at least one other α-olefin under slurry or gas phase polymerization conditions and at a higher polymerization reaction temperature than used in step (A) in the presence of a heterogeneous Ziegler catalyst in at least one other reactor to produce a second interpolymer which has a broad composition distribution (i.e. a composition distribution such that the composition has a homopolymer fraction as measured by the TREF technique and has multiple melting peaks), and a broad molecular weight distribution (i.e. a molecular weight distribution such that Mw/Mn is greater than 3), wherein 10 weight percent or more of the second interpolymer has a degree of branching of less than 2 methyls/1000 carbons, and wherein 25 weight percent or less of the second interpolymer has a degree of branching of 25 methyls/1000 carbons or more, wherein the Ziegler catalyst comprises. (i) a solid support component derived from a magnesium halide or silica, and (ii) a transition metal component represented by the formula: TrX'4-q(OR1)q, TrX'4-q(R2)q, VOX'3 or VO(OR1)3, wherein: TR is a Group, IVB, VB, or VIB metal, q is 0 or a number equal to or less than 4, X' is a halogen, and R1 is an alkyl group, aryl group or cycloalkyl group having from 1 to 20 carbon atoms, and R2 is an alkyl group, aryl group, aralkyl group, or substituted aralkyl group, and (C) combining the first interpolymer with the second interpolymer to form a polymer comprising the ethylene-α-olefin interpolymer composition, and (D) if necessary, removing the solvent from the polymer solution of step (C) and recovering the ethylene-α-olefin interpolymer composition. These polymerizations are carried out under slurry or gas plase conditions. The homogeneous catalyst is chosen from those metallocene-type catalysts which are capable of producing ethylene/α-olefin interpolymers of sufficiently high molecular weight under slurry or gas plase process polymerisation conditions. The heterogeneous catalyst is also chosen from those catalysts which are capable of efficiently producing the polymers under high temperature slurry or gas phase process conditions. In a second aspect of the invention, there is provided a process for preparing an ethylene/α-olefin interpolymer composition, characterized by: (A) polymerizing ethylene and at least one other α-olefin under slurry or gas phase polymerization conditions in at least one reactor containing a homogeneous catalyst composition to produce a solution of a first interpolymer which has a narrow composition distribution, (i.e., one which has a composition distribution branch index (CDBI) of greater than 50 percent where CDBI is defined at the weight percentage of polymer molecules having a comonomer content within 50 percent of the median total comonomer content as measured by the TREF technique defined herein), and a narrow molecular weight distribution (i.e. a molecular weight distribution such that Mw/Mn is less than 3), wherein 15% or less of the first interpolymer has a degree of branching of less than or equal to 2 methyls/1000 carbons and is lacking a measurable homopolymer fraction as measured by the TREF technique, and wherein the homogeneous catalyst composition contains either no aluminum cocatalyst or contains an amount of aluminum cocatalyst which will give rise to a detectable aluminum residue in the product of less than or equal to 250 ppm, (B) sequentially passing the interpolymer of (A) into at least one other reactor containing a heterogeneous Ziegler catalyst, ethylene and at least one other α-olefin, under slurry or gas phase polymerization conditions and at a higher polymerization reaction temperature than used in step (A) to produce the ethylene/α-olefin interpolymer composition, wherein the Ziegler catalyst comprises (i) a solid support component derived from a magnesium halide or silica, and (ii) a transition metal component represented by the formula: TrX'4-q(OR1)q, TrX'4-q(R2)q, VOX'3 or VO(OR1)3, wherein: TR is a Group, IVB, VB, or VIB metal, q is 0 or a number equal to or less than 4, X' is a halogen, and R1 is an alkyl group, aryl group or cycloalkyl group having from 1 to 20 carbon atoms, and R2 is an alkyl group, aryl group, aralkyl group, or substituted aralkyl group, and (C) combining the first interpolymer with the second interpolymer to form a polymer comprising the ethylene-α-olefin interpolymer composition, and (D) if necessary removing the solvent from the polymer of step (C) and recovering the ethylene-α-olefin interpolymer composition. In either process, the homogeneous catalyst composition preferably exhibits a high reactivity ratio and very readily incorporates higher α-olefins. The homogeneous catalysts employed in the production of the homogeneous ethylene interpolymer are desirably derived from monocyclopentadienyl complexes of the Group IV transition metals which contain a pendant bridging group attached to the cyclopentadienyl ring which acts as a bident ligand. Complex derivatives of titanium in the +3 or +4 oxidation state are preferred. In another aspect of this invention, there are provided novel interpolymers of ethylene and at least one a-olefin, wherein the interpolymers have controlled composition and molecular weight distributions. The, interpolymers have improved mechanical, thermal and optical properties and, surprisingly, the polymer compositions obtained by the processes described herein provide superior properties to materials obtained by merely blending the solid polymers obtained from process step (A) or (B) individually, in the First Process listed above. The novel polymer compositions of the present invention can be ethylene homopolymers or, preferably, interpolymers of ethylene with at least one C 3 -C 20 a-olefin and/or C 4 -C 18 diolefins. Interpolymers of ethylene and 1-octene are especially preferred. The term "interpolymer" is used herein to indicate a copolymer, or a terpolymer, or the like. That is, at least one other comonomer is polymerized with ethylene to make the interpolymer. Detailed Description of the Invention The homogeneous interpolymers used in the present invention are herein defined as defined in USP 3,645,992 (Elston). Accordingly, homogeneous polymers and interpolymers are those in which the comonomer is randomly distributed within a given interpolymer molecule and wherein substantially all of the interpolymer molecules have the same ethylene/comonomer ratio within that interpolymer, whereas heterogeneous interpolymers are those in which the interpolymer molecules do not have the same ethylene/comonomer ratio. The term "narrow composition distribution" used herein describes the comonomer distribution for homogeneous interpolymers and means that the homogeneous interpolymers have only a single melting peak and essentially lack a measurable "linear" polymer fraction. The narrow composition distribution homogeneous interpolymers can also be characterized by their SCBDI (Short Chain Branch Distribution Index) or CDBI (Composition Distribution Branch Index). The SCBDI or CBDI is defined as the weight percent of the polymer molecules having a comonomer content within 50 percent of the median total molar comonomer content. The CDBI of a polymer is readily calculated from data obtained from techniques known in the art, such as, for example, temperature rising elution fractionation (abbreviated herein as "TREF") as described, for example, in Wild et al, Journal of Polymer Science , Poly. Phys, Ed. , Vol. 20, p. 441 (1982), or in U.S. Patent 4,798,081. The SCBDI or CDBI for the narrow composition distribution homogeneous interpolymers and copolymers of the present invention is preferably greater than 30 percent, especially greater than 50 percent. The narrow composition distribution homogeneous interpolymers and copolymers used in this invention essentially lack a measurable "high density" (i.e., "linear" or homopolymer) fraction as measured by the TREF technique. The homogeneous interpolymers have a degree of branching less than or equal to 2 methyls/1000 carbons in 15 percent (by weight) or less preferably less than 10 percent (by weight), and especially less than 5 percent (by weight). The term "broad composition distribution" used herein describes the comonomer distribution for heterogeneous interpolymers and means that the heterogeneous interpolymers have a "linear" fraction and that the heterogeneous interpolymers have multiple melting peaks (i.e., exhibit at least two distinct melting peaks). The heterogeneous interpolymers and polymers have a degree of branching less than or equal to 2 mechyls/1000 carbons in 10 percent (by weight) or more, preferably more than 15 percent (by weight), and especially more than 20 percent (by weight). The heterogeneous interpolymers also have a degree of branching equal to or greater than 25 methyls/1000 carbons in 25 percent or less (by weight), preferably less than 15 percent (by weight), and especially less than 10 percent (by weight). The homogeneous interpolymers used to make the novel polymer compositions of the present invention are preferably interpolymers of ethylene with at least one C 3 -C 20 a-olefin and/or C 4 -C 18 diolefins. Homogeneous copolymers of ethylene and propylene, butene-1, hexene-1, 4-methyl-1-pentene and octene-1 are preferred and copolymers of ethylene and 1-octene are especially preferred. The homogeneous ethylene interpolymer and the heterogeneous ethylene interpolymer used in the compositions described herein can each be made separately in different reactors, and subsequently blended together to make the interpolymer compositions of the present invention. Preferably, though, the homogeneous ethylene polymer and the heterogeneous ethylene polymer used in the compositions described herein are made in a multiple reactor scheme, operated either in parallel or in series. In the multiple reactor scheme, at least one of the reactors makes the homogeneous ethylene interpolymer and at least one of the reactors makes the heterogeneous ethylene interpolymer. In a preferred mode of operation, the reactors are operated in a series configuration to make most advantage of the high polymerization temperatures allowed by the heterogeneous catalyst. When the reactors are connected in series, the polymerization reaction product from step (A) is fed directly (i.e., sequentially) into the reactor(s) for step (B) along with the ethylene/a-olefin reactants and heterogenous catalyst and solvent. Other unsaturated monomers usefully polymerized according to the present invention include, for example, ethylenically unsaturated monomers, conjugated or nonconjugated dienes, polyenes, etc. Preferred monomers include the C 2 -C 10 a-olefins especially ethylene, 1-propene, 1-butene, 1-hexene, 4-methyl-1-pentene, and 1-octene. Other preferred monomers include styrene, halo- or alkyl substituted styrenes, vinylbenzocyclobutane, 1,4-hexadiene, cyclopentene, cyclohexene and cyclooctene. The density of the ethylene interpolymer compositions of the present invention is measured in accordance with ASTM D-792 and is generally from 0.87 g/cm 3 to 0.965 g/cm 3 , preferably from 0.88 g/cm 3 to 0.95 g/cm 3 , and especially from 0.9 g/cm 3 to 0.935 g/cm 3 . The density of the homogeneous ethylene polymer used to make the ethylene polymer compositions is generally from 0.865 g/cm 3 to 0.92 g/cm 3 , preferably from 0.88 g/cm 3 to 0.915 g/cm 3 , and especially from 0.89 g/cm 3 to 0.91 g/cm 3 . The density of the heterogeneous ethylene polymer used to make the ethylene polymer compositions is generally from 0.9 g/cm 3 to 0.965 g/cm 3 , preferably from 0.9 g/cm 3 to 0.95 g/cm 3 , and especially from 0.915 g/cm 3 to 0.935 g/cm 3 . Generally, the amount of the ethylene interpolymer produced using the homogeneous catalyst and incorporated into the ethylene interpolymer composition is from 15 percent to 85 percent, by weight of the composition, preferably 25 percent to 75 percent, by weight of the composition. The molecular weight of the ethylene interpolymer compositions for use in the present invention is conveniently indicated using a melt index measurement according to ASTM D-1238, Condition 190 C/2.16 kg (formally known as "Condition (E)" and also known as I 2 ). Melt index is inversely proportional to the molecular weight of the polymer. Thus, the higher the molecular weight, the lower the melt index, although the relationship is not linear. The melt index for the ethylene interpolymer compositions used herein is generally from 0.1 grams/10 minutes (g/10 min) to 100 g/10 min, preferably from 0.3 g/10 min to 30 g/10 min, and especially from 0.5 g/10 min to 10 g/10 min. Additives such as antioxidants (e.g., hindered phenolics (e.g., Irganox® 1010 made by Ciba Geigy Corp.), phosphites (e.g., Irgafos® 168 also made by Ciba Geigy Corp.)), cling additives (e.g., polyisobutylene (PIB)), antiblock additives, and pigments can also be included in the polyethylene compositions, to the extent that they do not interfere with the enhanced composition properties discovered by Applicants. The Homogeneous Catalysts The homogeneous catalysts used in the invention are based on those monocyclopentadienyl transition metal complexes described in the art as constrained geometry metal complexes. These catalysts are highly efficient, meaning that they are efficient enough such that the catalyst residues left in the polymer do not influence the polymer quality. Typically, less than or equal to 10 ppm of the metal atom (designated herein as "M") is detectable and, when using the appropriate cocatalyst (e.g., one of the aluminoxanes described herein) the detectable aluminum residue is less than or equal to 250 ppm. Suitable constrained geometry catalysts for use herein preferably include constrained geometry catalysts as disclosed in European patent publication 416,815. The monocyclopentadienyl transition metal olefin polymerization catalysts taught in USP 5,026,798 (Canich) are also suitable for use in preparing the polymers of the present invention. The foregoing catalysts may be further described as comprising a metal coordination complex comprising a metal of group 4 of the Periodic Table of the Elements and a delocalized π-bonded moiety substituted with a constrain-inducing moiety, said complex having a constrained geometry about the metal atom such that the angle at the metal between the centroid of the delocalized, substituted π-bonded moiety and the center of at least one remaining substituent is less than such angle in a similar complex containing a similar π-bonded moiety lacking in such constrain-inducing substituent, and provided further that for such complexes comprising more than one delocalized, substituted π-bonded moiety, only one thereof for each metal atom of the complex is a cyclic, delocalized, substituted π-bonded moiety. The catalyst further comprises an activating cocatalyst. Preferred catalyst complexes correspond to the formula: wherein: M is a metal of group 4 of the Periodic Table of the Elements; Cp* is a cyclopentadienyl or substituted cyclopentadienyl group bound in an h 5 bonding mode to M; Z is a moiety comprising boron, or a member of group 14 of the Periodic Table of the Elements, and optionally sulfur or oxygen, said moiety having up to 20 non-hydrogen atoms, and optionally Cp* and Z together form a fused ring system; X independently each occurrence is an anionic ligand group having up to 30 non-hydrogen atoms; n is 1 or 2; and Y is an anionic or nonanionic ligand group bonded to Z and M comprising nitrogen, phosphorus, oxygen or sulfur and having up to 20 non-hydrogen atoms, optionally Y and Z together form fused ring system. More preferably still, such complexes correspond to the formula: wherein: R' each occurrence is independently selected from the group consisting of hydrogen, alkyl, aryl, and silyl, and combinations thereof having up to 20 non-hydrogen atoms; X each occurrence independently is selected from the group consisting of hydride, halo, alkyl, aryl, silyl, aryloxy, alkoxy, amide, siloxy and combinations thereof having up to 20 non-hydrogen atoms; Y is -O-, -S-, -NR*-, -PR*-, or a neutral two electron donor ligand selected from the group consisting of OR*, SR*, NR* 2 or PR* 2 ; M is as previously defined; and Z is SiR* 2 , CR* 2 , SiR* 2 SiR* 2 , CR* 2 CR* 2 , CR*=CR*, CR* 2 SiR* 2 , BR*; wherein R* each occurrence is independently selected from the group consisting of hydrogen, alkyl. aryl, silyl groups having up to 20 non-hydrogen atoms, and mixtures thereof, or two or more R* groups from Y, Z, or both Y and Z form a fused ring system; and n is 1 or 2. Most highly preferred complex compounds are amidosilane- or amidoalkanediyl- compounds corresponding to the formula: wherein: M is titanium, zirconium or hafnium, bound in an h 5 bonding mode to the cyclopentadienyl group; R' each occurrence is independently selected from the group consisting of hydrogen, alkyl and aryl and combinations thereof having up to 7 carbon atoms, or silyl; E is silicon or carbon; X independently each occurrence is hydride, halo, alkyl, aryl, aryloxy or alkoxy of up to 10 carbons, or silyl; m is 1 or 2; and n is 1 or 2. Examples of the above most highly preferred metal coordination compounds include compounds wherein the R' on the amido group is methyl, ethyl, propyl, butyl, pentyl, hexyl, (including isomers), norbornyl, benzyl, phenyl, etc.; the cyclopentadienyl group is cyclopentadienyl, indenyl, tetrahydroindenyl, fluorenyl, octahydrofluorenyl, etc.; R' on the foregoing cyclopentadienyl groups each occurrence is hydrogen, methyl, ethyl, propyl, butyl, pentyl, hexyl, (including isomers), norbornyl, benzyl, phenyl, etc.; and X is chloro, bromo, iodo, methyl, ethyl, propyl, butyl, pentyl, hexyl, (including isomers), norbornyl, benzyl, phenyl, etc. Specific compounds include: (tert-butylamido)(tetramethyl-h 5 -cyclopentadienyl)-1,2-ethanediylzirconium dichloride, (tert-butylamido) (tetramethyl-h 5 -cyclopentadienyl)-1,2-ethanediyltitanium dichloride, (methylamido)(tetramethyl-h 5 -cyclopentadienyl)-1,2-ethanediylzirconium dichloride, (methylamido)(tetramethyl-h 5 -cyclopentadienyl)-1,2-ethanediyltitanium dichloride, (ethylamido)(tetramethyl-h 5 -cyclopentadienyl)methylenetitanium dichloride, (tertbutylamido)dibenzyl(tetramethyl-h 5 -cyclopentadienyl) silanezirconium dibenzyl, (benzylamido)dimethyl- (tetramethyl-h 5 -cyclopentadienyl)silanetitanium dichloride, (phenylphosphido)dimethyl(tetramethyl-h 5 -cyclopentadienyl)silanezirconium dibenzyl, (tertbutylamido)dimethyl(tetramethyl-h 5 -cyclopentadienyl)silanetitanium dimethyl, and the like. The catalyst compositions are derived from reacting the metal complex compounds with a suitable activating agent or cocatalyst or combination of cocatalysts. Suitable cocatalysts for use herein include polymeric or oligomeric aluminoxanes, especially aluminoxanes soluble in non-aromatic hydrocarbon solvent, as well as inert, compatible, noncoordinating, ion forming compounds; or combinations of polymeric/oligomeric aluminoxanes and inert, compatible, noncoordinating, ion forming compounds. Preferred cocatalysts contain inert, noncoordinating, boron compounds. Ionic active catalyst species which can be used to polymerize the polymers described herein correspond to the formula: wherein: M is a metal of group 4 of the Periodic Table of the Elements; Cp* is a cyclopentadienyl or substituted cyclopentadienyl group bound in an h 5 bonding mode to M; Z is a moiety comprising boron, or a member of group 14 of the Periodic Table of the Elements, and optionally sulfur or oxygen, said moiety having up to 20 non-hydrogen atoms, and optionally Cp* and Z together form a fused ring system; X independently each occurrence is an anionic ligand group having up to 30 non-hydrogen atoms; n is 1 or 2; and A- is a noncoordinating, compatible anion. One method of making the ionic catalyst species which can be utilized to make the polymers of the present invention involve combining: a) at least one first component which is a mono(cyclopentadienyl) derivative of a metal of Group 4 of the Periodic Table of the Elements as described previously containing at least one substituent which will combine with the cation of a second component (described hereinafter) which first component is capable of forming a cation formally having a coordination number that is one less than its valence, and b) at least one second component which is a salt of a Bronsted acid and a noncoordinating, compatible anion. Compounds useful as a second component in the preparation of the ionic catalysts useful in this invention can comprise a cation, which is a Bronsted acid capable of donating a proton, and a compatible noncoordinating anion. Preferred anions are those containing a single coordination complex comprising a charge-bearing metal or metalloid core which anion is relatively large (bulky), capable of stabilizing the active catalyst species (the Group 4 cation) which is formed when the two components are combined and sufficiently labile to be displaced by olefinic, diolefinic and acetylenically unsaturated substrates or other neutral Lewis bases such as ethers, nitriles and the like. Compounds containing anions which comprise coordination complexes containing a single metal or metalloid atom are, of course, well known and many, particularly such compounds containing a single boron atom in the anion portion, are available commercially. In light of this, salts containing anions comprising a coordination complex containing a single boron atom are preferred. Highly preferably, the second component useful in the preparation of the catalysts of this invention may be represented by the following general formula: (L-H) + [A] - wherein: L is a neutral Lewis base; (L-H) + is a Bronsted acid; and [A] - is a compatible, noncoordinating anion. More preferably [A] - corresponds to the formula: [BQ q ] - wherein: B is boron in a valence state of 3; and Q independently each occurrence is selected from the Group consisting of hydride, dialkylamido, halide, alkoxide, aryloxide, hydrocarbyl, and substituted-hydrocarbyl radicals of up to 20 carbons with the proviso that in not more than one occurrence is Q halide. Illustrative, but not limiting, examples of boron compounds which may be used as a second component in the preparation of the improved catalysts of this invention are trialkyl-substituted ammonium salts such as triethylammonium tetraphenylborate, tripropylammonium tetraphenylborate, tris(n-butyl)ammonium tetraphenylborate, trimethylammonium tetrakis(p-tolyl)borate, tributylammonium tetrakis(pentafluorophenyl)borate, tripropylammonium tetrakis(2,4-dimethylphenyl)borate, tributylammonium tetrakis(3,5-dimethylphenyl)borate, triethylammonium tetrakis(3,5-di-trifluoromethylphenyl)borate and the like. Also suitable are N,N-dialkylanilinium salts such as N,N-dimethylanilinium tetraphenylborate, N,N-diethylanilinium tetraphenylborate, N,N,2,4,6-pentamethylanilinium tetraphenylborate and the like; dialkylammonium salts such as di(i-propyl)ammonium tetrakis(pentafluorophenyl)borate, dicyclohexylammonium tetraphenylborate and the like; and triarylphosphonium salts such as triphenylphosphonium tetraphenylborate, tris(methylphenyl)phosphonium tetrakis(pentafluorophenyl)borate, tris(dimethylphenyl)phosphonium tetraphenylborate and the like. Preferred ionic catalysts are those having a limiting charge separated structure corresponding to the formula: wherein: M is a metal of group 4 of the Periodic Table of the Elements; Cp* is a cyclopentadienyl or substituted cyclopentadienyl group bound in an h 5 bonding mode to M; Z is a moiety comprising boron, or a member of group 14 of the Periodic Table of the Elements, and optionally sulfur or oxygen, said moiety having up to 20 non-hydrogen atoms, and optionally Cp* and Z together form a fused ring system; X independently each occurrence is an anionic ligand group having up to 30 non-hydrogen atoms; n is 1 or 2; and XA* - is - X(B(C 6 F 5 ) 3 ). This class of cationic complexes can also be conveniently prepared by contacting a metal compound corresponding to the formula: wherein: Cp*, M, and n are as previously defined, with tris(pentafluorophenyl)borane cocatalyst under conditions to cause abstraction of X and formation of the anion - X(B(C 6 F 5 ) 3 ). Preferably X in the foregoing ionic catalyst is C 1 -C 10 hydrocarbyl, most preferably methyl or benzyl. The preceding formula is referred to as the limiting, charge separated structure. However, it is to be understood that, particularly in solid form, the catalyst may not be fully charge separated. That is, the X group may retain a partial covalent bond to the metal atom, M. Thus, the catalysts may be alternately depicted as possessing the formula: The catalysts are preferably prepared by contacting the derivative of a Group 4 metal with the tris(pentafluorophenyl)borane in an inert diluent such as an organic liquid. Tris(pentafluorphenyl)borane is a commonly available Lewis acid that may be readily prepared according to known techniques. The compound is disclosed in Marks, et al. J. Am. Chem. Soc. 1991, 113, 3623-3625 for use in alkyl abstraction of zirconocenes. The homogeneous catalyst can contain either no aluminum cocatalyst or only a small amount (i.e., from 3:1 Al:M ratio to 100:1 Al:M ratio) of aluminum cocatalyst. For example, the cationic complexes used as homogeneous catalysts may be further activated by the use of an additional activator such as an alkylaluminoxane. Preferred co-activators include methylaluminoxane, propylaluminoxane, isobutylaluminoxane, combinations thereof and the like. So-called modified methylaluminoxane (MMAO) is also suitable for use as a cocatalyst. One technique for preparing such modified aluminoxane is disclosed in U.S. Patent 4,960,878 (Crapo et al.). Aluminoxanes can also be made as disclosed in U.S. Patents Nos. 4,544,762 (Kaminsky et al.) ; 5,015,749 (Schmidt et al.); 5,041,583 (Sangokoya); 5,041,584 (Crapo et al.); and 5,041,585 (Deavenport et al.). The homogeneous catalysts useful for the production of the ethylene interpolymers of narrow composition and molecular weight distribution may also be supported on an inert support. Typically, the support can be any solid, particularly porous supports such as talc or inorganic oxides, or resinous support materials such as a polyolefin. Preferably, the support material is an inorganic oxide in finely divided form. Suitable inorganic oxide materials which are desirably employed in accordance with this invention include Group IIA, IIIA, IVA, or IVB metal oxides such as silica, alumina, and silica-alumina and mixtures thereof. Other inorganic oxides that may be employed either alone or in combination with the silica, alumina or silica-alumina are magnesia, titania, zirconia, and the like. Other suitable support materials, however, can be employed, for example, finely divided polyolefins such as finely divided polyethylene. The metal oxides generally contain acidic surface hydroxyl groups which will react with the homogeneous catalyst component added to the reaction slurry. Prior to use, the inorganic oxide support is dehydrated, i.e., subjected to a thermal treatment in order to remove water and reduce the concentration of the surface hydroxyl groups. The treatment is carried out in vacuum or while purging with a dry inert gas such as nitrogen at a temperature of 100°C to 1000°C, and preferably, from 300°C to 800°C. Pressure considerations are not critical. The duration of the thermal treatment can be from 1 to 24 hours; however, shorter or longer times can be employed provided equilibrium is established with the surface hydroxyl groups. The Heterogeneous Catalysts The heterogeneous catalysts suitable for use in the invention are typical supported, Ziegler-type catalysts which are particularly useful at the high polymerization temperatures of the solution process. Examples of such compositions are those derived from organomagnesium compounds, alkyl halides or aluminum halides or hydrogen chloride, and a transition metal compound. Examples of such catalysts are described in U.S. Pat Nos. 4,314,912 (Lowery, Jr. ct al.), 4,547,475 (Class et al.), and 4,612,300 (Coleman, III). Particularly suitable organomagnesium compounds include, for example, hydrocarbon soluble dihydrocarbylmagnesium such as the magnesium dialkyls and the magnesium diaryls. Exemplary suitable magnesium dialkyls include particularly n-butyl-sec-butylmagnesium, diisopropylmagnesium, di-n-hexylmagnesium, isopropyl-n-butyl-magnesium, ethyl-n-hexylmagnesium, ethyl-n-butylmagnesium, di-n-octylmagnesium and others wherein the alkyl has from 1 to 20 carbon atoms. Exemplary suitable magnesium diaryls include diphenylmagnesium, dibenzylmagnesium and ditolylmagnesium. Suitable organomagnesium compounds include alkyl and aryl magnesium alkoxides and aryloxides and aryl and alkyl magnesium halides with the halogen-free organomagnesium compounds being more desirable. Among the halide sources which can be employed herein are the active non-metallic halides, metallic halides, and hydrogen chloride. Suitable non-metallic halides are represented by the formula R'X wherein R' is hydrogen or an active monovalent organic radical and X is a halogen. Particularly suitable non-metallic halides include, for example, hydrogen halides and active organic halides such as t-alkyl halides, allyl halides, benzyl halides and other active hydrocarbyl halides wherein hydrocarbyl is as defined hereinbefore. By an active organic halide is meant a hydrocarbyl halide that contains a labile halogen at least as active, i.e., as easily lost to another compound, as the halogen of sec-butyl chloride, preferably as active as t-butyl chloride. In addition to the organic monohalides, it is understood that organic dihalides, trihalides and other polyhalides that are active as defined hereinbefore are also suitably employed. Examples of preferred active non-metallic halides include hydrogen chloride, hydrogen bromide, t-butyl chloride, t-amyl bromide, allyl chloride, benzyl chloride, crotyl chloride, methylvinyl carbinyl chloride, a-phenylethyl bromide, diphenyl methyl chloride and the like. Most preferred are hydrogen chloride, t-butyl chloride, allyl chloride and benzyl chloride. Suitable metallic halides which can be employed herein include those represented by the formula MR y-a X a wherein: M is a metal of Groups IIB, IIIA or IVA of Mendeleev's Periodic Table of Elements, R is a monovalent organic radical, X is a halogen, Y has a value corresponding to the valence of M, and a has a value from 1 to y. Preferred metallic halides are aluminum halides of the formula AlR 3-a X a wherein: each R is independently hydrocarbyl as hereinbefore defined such as alkyl, X is a halogen and a is a number from 1 to 3. Most preferred are alkylaluminum halides such as ethylaluminum sesquichloride, diethylaluminum chloride, ethylaluminum dichloride, and diethylaluminum bromide, with ethylaluminum dichloride being especially preferred. Alternatively, a metal halide such as aluminum trichloride or a combination of aluminum trichloride with an alkyl aluminum halide or a trialkyl aluminum compound may be suitably employed. It is understood that the organic moieties of the aforementioned organomagnesium, e.g., R*, and the organic moieties of the halide source, e.g., R and R', are suitably any other organic radical provided that they do not contain functional groups that poison conventional Ziegler catalysts. The magnesium halide can be preformed from the organomagnesium compound and the halide source or it can be formed in situ in which instance the catalyst is preferably prepared by mixing in a suitable solvent or reaction medium (1) the organomagnesium component and (2) the halide source, followed by the other catalyst components. Any of the conventional Ziegler-Natta transition metal compounds can be usefully employed as the transition metal component in preparing the supported catalyst component. Typically, the transition metal component is a compound of a Group IVB, VB, or VIB metal. The transition metal component is generally, represented by the formulas: TrX' 4-q (OR 1 ) q , TrX' 4-q R 2 q , VOX'3 and VO (OR 1 ) 3 . Tr is a Group IVB, VB, or VIB metal, preferably a Group IVB or VB metal, preferably titanium, vanadium or zirconium, q is 0 or a number equal to or less than 4. X' is a halogen, and R 1 is an alkyl group, aryl group or cycloalkyl group having from 1 to 20 carbon atoms, and R 2 is an alkyl group, aryl group, aralkyl group, substituted aralkyls, and the like. The aryl, aralkyls and substituted aralkys contain 1 to 20 carbon atoms, preferably 1 to 10 carbon atoms. When the transition metal compound contains a hydrocarbyl group, R 2 , being an alkyl, cycloalkyl, aryl, or aralkyl group, the hydrocarbyl group will preferably not contain an H atom in the position beta to the metal carbon bond. Illustrative but non-limiting examples of aralkyl groups are methyl, neo-pentyl. 2,2-dimethylbutyl, 2,2-dimethylhexyl; aryl groups such as benzyl; cycloalkyl groups such as 1-norbornyl. Mixtures of these transition metal compounds can be employed if desired. Illustrative examples of the transition metal compounds include TiCl 4 , TiBr 4 , Ti(OC 2 H 5 ) 3 Cl, Ti(OC 2 H 5 )Cl 3 , Ti(OC 4 H 9 ) 3 Cl, Ti(OC 3 H 7 ) 2 Cl 2 , Ti(OC 6 H 13 ) 2 Cl 2 , Ti(OC 8 H 17 ) 2 Br 2 , and Ti(OC 12 H 25 )Cl 3 , Ti(O-i-C 3 H 7 ) 4 , and Ti(O-n-C 4 H 9 ) 4 . Illustrative examples of vanadium compounds include VCl 4 , VOCl 3 , VO(OC 2 H 5 ) 3 , and VO (OC 4 H 9 ) 3 . Illustrative examples of zirconium compounds include ZrCl 4 , ZrCl 3 (OC 2 H 5 ), ZrCl 2 (OC 2 H 5 ) 2 , ZrCl(OC 2 H 5 ) 3 , Zr(OC 2 H 5 ) 4 , ZrCl 3 (OC 4 H 9 ), ZrCl 2 (OC 4 H 9 ) 2 , and ZrCl(OC 4 H 9 ) 3 . As indicated above, mixtures of the transition metal compounds may be usefully employed, no restriction being imposed on the number of transition metal compounds which may be contracted with the support. Any halogenide and alkoxide transition metal compound or mixtures thereof can be usefully employed. The previously named transition metal compounds are especially preferred with vanadium tetachloride, vanadium oxychloride, titanium tetraisopropoxide, titanium tetrabutoxide, and titanium tetrachloride being most preferred. Suitable catalyst materials may also be derived from a inert oxide supports and transition metal compounds. Examples of such compositions suitable for use in the solution polymerization process are described in U. S. Patent No. 5,231,151. The inorganic oxide support used in the preparation of the catalyst may be any particulate oxide or mixed oxide as previously described which has been thermally or chemically dehydrated such that it is substantially free of adsorbed moisture. The specific particle size, surface area, pore volume, and number of surface hydroxyl groups characteristic of the inorganic oxide are not critical to its utility in the practice of the invention. However, since such characteristics determine the amount of inorganic oxide to be employed in preparing the catalyst compositions, as well as affecting the properties of polymers formed with the aid of the catalyst compositions, these characteristics must frequently be taken into consideration in choosing an inorganic oxide for use in a particular aspect of the invention. In general, optimum results are usually obtained by the use of inorganic oxides having an average particle size in the range of 1 to 100 microns, preferably 2 to 20 microns; a surface area of 50 to 1,000 square meters per gram, preferably 100 to 400 square meters per gram; and a pore volume of 0.5 to 3.5 cm 3 per gram; preferably 0.5 to 2 cm 3 per gram. In order to further improve catalyst performance, surface modification of the support material may be desired. Surface modification is accomplished by specifically treating the support material such as silica, aluminia or silica-alumina with an organometallic compound having hydrolytic character. More particularly, the surface modifying agents for the support materials comprise the organometallic compounds of the metals of Group IIA and IIIA of the Periodic Table. Most preferably the organometallic compounds are selected from magnesium and aluminum organometallics and especially from magnesium and aluminum alkyls or mixtures thereof represented by the formulas and R 1 MgR 2 and R 1 R 2 AlR 3 wherein each of R 1 , R 2 and R 3 which may be the same or different are alkyl groups, aryl groups, cycloalkyl groups, aralkyl groups, alkoxidc groups, alkadienyl groups or alkenyl groups. The hydrocarbon groups R 1 , R 2 and R 3 can contain between 1 and 20 carbon atoms and preferably from 1 to about 10 carbon atoms. The surface modifying action is effected by adding the organometallic compound in a suitable solvent to a slurry of the support material. Contact of the organometallic compound in a suitable solvent and the support is maintained from 30 to 180 minutes and preferably from 60 to 90 minutes at a temperature in the range of 20° to 100° C. The diluent employed in slurrying the support can be any of the solvents employed in solubilizing the organometallic compound and is preferably the same. In order to more readily produce interpolymer compositions of controlled composition and molecular weight distribution, the constrained-geometry component catalyst and the Ziegler-type transition metal catalyst component should have different reactivity ratios. The reactivity ratio of the homogeneous catalyst may be higher than the reactivity ratio of the heterogeneous catalyst. In such instances, the contribution of the narrow composition and molecular weight distribution polymer molecules, formed in the first reactor, to the whole interpolymer product would yield improvements in thermal resistance and crystallization behavior of the resin. Preferably, but not limiting, the reactivity ratio of the homogeneous catalyst introduced into the first reactor should be lower than the reactivity ratio of the heterogeneous catalyst in order to have the most benefit of a simplified process and to produce interpolymers of the most suitable compositions. The reactivity ratios of the metallocenes and transition metal components in general are obtained by methods well known such as, for example, as described in "Linear Method for Determining Monomer Reactivity Ratios in Copolymerization", M. Fineman and S. D. Ross, J. Polymer Science 5, 259 (1950) or "Copolymerization", F. R. Mayo and C. Walling, Chem. Rev. 46, 191 (1950) . For example, to determine reactivity ratios, the most widely used copolymerization model is based on the following equations: here M 1 , M 2 refer to monomer molecules and M 1 * or M 2 * refer to a growing polymer chain to which monomer M 1 or M 2 has most recently attached. M 1 is typically ethylene; M 2 is typically an a-olefin comonomer. The k ij values are the rate constants for the indicated reactions. In this case, k 11 represents the rate at which an ethylene unit inserts into a growing polymer chain in which the previously inserted monomer unit was also ethylene. The reactivity rates follows as: r 1 =k 11 /k 12 and r 2 =k 22 /k 21 wherein k 11 , k 12 , k 22 , and k 21 are the rate constants for ethylene (1) or comonomer (2) addition to a catalyst site where the last polymerized monomer is ethylene (k 1X ) or comonomer (2) (k 2X ). A lower value of r 1 for a particular catalyst translates into the formation of an interpolymer of higher comonomer content produced in a fixed reaction environment. In a preferred embodiment of the invention, the reactivity ratio, r 1 , of the homogeneous catalyst is less than half that of the heterogeneous catalyst. Therefore, in the desirable practice of the invention, the homogeneous catalyst produces a polymer of higher comonomer content than that of the polymer produced by the heterogeneous in a reaction environment which is low in the concentration of the comonomer. As the contents of the first reactor enter a second reactor, the concentration of the comonomer in the second reactor is reduced. Hence, the reaction environment in which the heterogeneous catalyst forms polymer is such that a polymer containing a lower comonomer content is produced. Under such reaction conditions, the polymer so formed with have a well-defined and narrow composition distribution and narrow molecular weight distribution. The resulting whole interpolymer product can be readily controlled by choice of catalysts, comonomers, and reaction temperatures in an economical and reproducible fashion. In addition, simple changes in monomer concentrations and conversions in each reactor allows the manufacture of a broad range of interpolymer products. The heterogeneous polymers and interpolymers used to make the novel polymer compositions of the present invention can be ethylene homopolymers or, preferably, interpolymers of ethylene with at least one C 3 -C 20 a-olefin and/or C 4 -C 18 diolefins. Heterogeneous copolymers of ethylene and 1-octene are especially preferred. Polymerization The polymerization conditions for manufacturing the polymers of the present invention are generally those useful in slurry and gas phase polymerization processes. The proper catalysts and polymerization conditions must be employed. Multiple reactor polymerization processes are particularly useful in the present invention, such as those disclosed in USP 3,914,342 (Mitchell). The multiple reactors can be operated in series or in parallel, with at least one constrained geometry catalyst employed in one of the reactors and at least one heterogeneous catalyst employed in at least one other reactor. Preferably, the polymerization temperature of the constrained geometry portion of the polymerization is lower than that of the heterogeneous polymerization portion of the reaction. According to one embodiment of the present process, the polymers are produced in a continuous process, as opposed to a batch process. Preferably, the polymerization temperature is from 20°C to 250°C, using constrained geometry catalyst technology. In the generally preferred embodiments where a narrow molecular weight distribution polymer (M w /M n of from 1.5 to 2.5) having a higher I 10 /I 2 ratio (e.g., I 10 /I 2 of at least 7, preferably at least 8, especially at least 9) is desired, the ethylene concentration in the reactor is preferably not more than 8 percent by weight of the reactor contents, especially not more than 4 percent by weight of the reactor contents. Generally, manipulation of I 10 /I 2 while holding M w /M n relatively low for producing the polymers described herein is a function of reactor temperature and/or ethylene concentration. Reduced ethylene concentration and higher temperature generally produce higher I 10 /I 2 materials. Molecular Weight Distribution Determination The interpolymer product samples analyzed by gel permeation chromatography (GPC) on a Waters 150C high temperature chromatographic unit equipped with three mixed porosity columns (Polymer Laboratories 10 3 , 10 4 , 10 5 , and 10 6 ), operating at a system temperature of 140°C. The solvent is 1,2,4-trichlorobenzene, from which 0.3 percent by weight solutions of the samples are prepared for injection. The flow rate is 1.0 milliliters/minute and the injection size is 200 microliters. The molecular weight determination is deduced by using narrow molecular weight distribution polystyrene standards (from Polymer Laboratories) in conjunction with their elution volumes. The equivalent polyethylene molecular weights are determined by using appropriate Mark-Houwink coefficients for polyethylene and polystyrene (as described by Williams and Word in Journal of Polymer Science , Polymer Letters, Vol. 6, (621) 1968) to derive the following equation: M polyethylene = a * (M polystyrene ) b . In this equation, a = 0.4316 and b = 1.0. Weight average molecular weight, M w , is calculated in the usual manner according to the following formula: M w = R w i * M i , where w i and M i are the weight fraction and molecular weight, respectively, of the ith fraction eluting from the GPC column. For the interpolymer fractions and whole interpolymers described herein, the term "narrow molecular weight distribution" means that the M w /M n of the interpolymer (or fraction) is less than 3, preferably from 2 to 3. The M w /M n of the "narrow molecular weight distribution" interpolymer (or fraction) can also be described by the following equation: (M w /M n ) ≤ (I 10 /I 2 ) - 4.63. For the interpolymer fractions and whole interpolymers described herein, the term "broad molecular weight distribution" means that the M w /M n of the interpolymer (or fraction) is greater than 3, preferably from 3 to 5. Crystallization Onset Temperature Measurement The crystallization onset temperatures of the polyethylene compositions described herein are measured using differential scanning calorimetry (DSC). Each sample to be tested is made into a compression molded plaque according to ASTM D 1928. The plaques are then thinly sliced at room temperature using a Reichert Microtome or a razor blade to obtain samples having a thickness of about 15 micrometers. About 5 milligrams of each sample to be tested is placed in the DSC pan and heated to about 180°C, held at that temperature for 3 minutes to destroy prior heat history, cooled to -50°C at a rate of 10°C/minute and held at that temperature for 2 minutes. The crystallization onset temperature and the peak temperature are recorded by the DSC as the temperature at which crystallization begins and the temperature at which the sample is as fully crystallized as possible, respectively, during the cooling period from 180°C to -50°C. Other useful physical property determinations made on the novel interpolymer compositions described herein include: Melt flow ratio (MFR): measured by determining "I 10 " (according to ASTM D-1238, Condition 190°C/10 kg (formerly known as "Condition (N)") and dividing the obtained I 10 by the I 2 . The ratio of these two melt index terms is the melt flow ratio and is designated as I 10 /I 2 . For the homogeneous portion of the interpolymer composition, the I 10 /I 2 ratio is generally greater than or equal to 5.63 and preferably from 5.8 to 8.5. For the heterogeneous portion of the interpolymer composition, the I 10 /I 2 ratio is typically from 6.8 to 9.5. The I 10 /I 2 ratio for the whole interpolymer compositions is typically from 6.8 to 10.5. 2% Secant Modulus: using a method similar to ASTM D 882, except that 4 specimens are used, a 4 (18 cm) inch gauge length is used and the conditioning period is 24 hours; Clarity: measured by specular transmittance according to ASTM D 1746, except that the samples are conditioned for 24 hours; Haze: measured according to ASTM D 1003. Young's modulus, yield strength and elongation, break strength and elongation, and toughness: using a method similar to ASTM D 882, except that 4 specimens are used and are pulled at 20 inches per minute (50 cm/min) using a 2 inch (5 cm) gauge length; Spencer Impact: using a method similar to ASTM D 3420, procedure "B", except that the maximum capacity is 1600 grams, the values are normalized for sample thickness and the conditioning period has been shortened from 40 hours to 24 hours; and Tensile Tear: using a method similar to ASTM D 1938, except that 4 specimens are used. Useful articles which can be made from such interpolymer compositions include films (e.g., cast film, blown film or extrusion coated types of film), fibers (e.g., staple fibers, melt blown fibers or spunbonded fibers (using, e.g., systems as disclosed in USP 4,340,563, USP 4,663,220, USP 4,668,566, or USP 4,322,027), and gel spun fibers (e.g., the system disclosed in USP 4,413,110)), both woven and nonwoven fabrics (e.g., spunlaced fabrics disclosed in USP 3,485,706) or structures made from such fibers (including, e.g., blends of these fibers with other fibers, e.g., PET or cotton)), and molded articles (e.g., blow molded articles, injection molded articles and rotomolded articles). Films particularly benefit from such interpolymer compositions. Films and film structures having the novel properties described herein can be made using conventional hot blown film fabrication techniques or other biaxial orientation process such as tenter frames or double bubble processes. Conventional hot blown film processes are described, for example, in The Encyclopedia of Chemical Technology . Kirk-Othmer, Third Edition, John Wiley & Sons, New York, 1981, Vol. 16, pp. 416-417 and Vol. 18, pp. 191-192. Biaxial orientation film manufacturing process such as described in a "double bubble" process as in U.S. Patent 3,456,044 (Pahlke), and the processes described in U.S. Patent 4,865,902 (Golike et al.), U.S. Patent 4,352,849 (Mueller), U.S. Patent 4,620,557 (Warren), U.S. Patent 4,927,708 (Herran et al.), U.S. Patent 4,963,419 (Lustig et al.), and U.S. Patent 4,952,451 (Mueller) can also be used to make novel film structures from the novel interpolymer compositions. Novel property combinations of such films include unexpectedly high machine and cross direction secant modulus, both first and second machine and cross direction yield, dart impact, cross direction tensile, clarity, 20° gloss, 45° gloss, low haze, low blocking force and low coefficient of friction (COF). In addition, these interpolymer compositions have better resistance to melt fracture. An apparent shear stress vs. apparent shear rate plot is used to identify the melt fracture phenomena. According to Ramamurthy in Journal of Rheology , 30(2), 337-357, 1986, above a certain critical flow rate, the observed extrudate irregularities may be broadly classified into two main types: surface melt fracture and gross melt fracture. Surface melt fracture occurs under apparently steady flow conditions and ranges in detail from loss of specular gloss to the more severe form of "sharkskin". In this disclosure, the onset of surface melt fracture is characterized at the beginning of losing extrudate gloss at which the surface roughness of extrudate can only be detected by 40X magnification. The critical shear rate at onset of surface melt fracture for the substantially linear olefin polymers is at least 50 percent greater than the critical shear rate at the onset of surface melt fracture of a linear olefin polymer having about the same 12 and Mw/Mn. Gross melt fracture occurs at unsteady flow conditions and ranges in detail from regular (alternating rough and smooth, helical, etc.) to random distortions. For commercial acceptability, (e.g., in blown film products), surface defects should be minimal, if not absent. The critical shear rate at onset of surface melt fracture (OSMF) and onset of gross melt fracture (OGMF) will be used herein based on the changes of surface roughness and configurations of the extrudates extruded by a GER. Example 1 Homogeneous Catalyst Preparation A known weight of the constrained-geometry organometallic complex [{(CH 3 ) 4 C 5 )}-(CH 3 ) 2 Si-N-(t-C 4 H 9 )]Ti(CH 3 ) 2 was dissolved in lsopar E to give a clear solution with a concentration of Ti of 0.005M. A similar solution of the activator complex, tris(perfluoropheny)borane (0.010M) was also prepared. A catalyst composition of a few mL total volume was prepared by adding 2.0 mL of Isopar E solution of Ti reagent, 2.0 mL of the borane (for B:Ti = 2:1) and 2 mL lsopar E to a 4 oz (100 ml) glass bottle. The solution was mixed for a few minutes and transferred by syringe to a catalyst injection cylinder on the polymerization reactor. Heterogeneous Catalyst Preparation A heterogeneous Ziegler-type catalyst was prepared substantially according to USP 4,612.300 (Ex. P.), by sequentially adding to a volume of Isopar E, a slurry of anhydrous magnesium chloride in Isopar E, a solution of EtAlCl 2 in hexane, and a solution of Ti(O-iPr) 4 in Isopar E, to yield a composition containing a magnesium concentration of 0.17M and a ratio of Mg/Al/Ti of 40/12/3. An aliquot of this composition containing 0.064 mmol of Ti which was treated with a dilute solution of Et 3 Al to give an active catalyst with a final Al/Ti ratio of 8/1. This slurry was then transferred to a syringe until it was required for injection into the polymerization reactor. The polymerization Examples which follow are examples of solution polymerization, and are therefore not directly illustrative of the claimed invention. They are nevertheless illustrative of the general techniques to be employed. They are therefore referred to as "Reference Examples". Reference Example 1 (Polymerization) The polymerization described in this example demonstrates a process for the use of two catalysts, employed sequentially, in two polymerization reactors. A stirred, one-gallon (3.79L) autoclave reactor is charged with 2.1 L of Isopar™ E (made by Exxon Chemical) and 388 mL of 1-octene comonomer and the contents are heated to 150°C. The reactor is next charged with ethylene sufficient to bring the total pressure to 450 psig (3.2 MPa). A solution containing 0.010 mmol of the active organometallic catalyst described in the catalyst preparation section is injected into the reactor using a high pressure nitrogen sweep. The reactor temperature and pressure are maintained constant at the desired final pressure and temperature by continually feeding ethylene during the polymerization run and cooling the reactor as necessary. After a 10 minute reaction time, the ethylene is shut off and the reactor is depressured to 100 psig (0.8 MPa). Hydrogen is admitted to the reactor and the contents heated. A slurry of the heterogeneous catalyst containing 0.0064 mmol Ti prepared as described in the catalyst preparation section is injected into the reactor using a high pressure nitrogen sweep. The reactor is then continually fed ethylene at 450 psig (3.2 MPa) and the reaction temperature quickly rose to 185°C where the polymerization is sustained for an additional 10 minutes. At this time the reactor is depressured and the hot polymer-containing solution transferred into a nitrogen-purged resin kettle containing 0.2 g Irganox 1010 antioxidant as a stabilizer. After removal of all the solvent in vacuo, the sample is then weighed (yield 270 g) to determine catalyst efficiencies (344300 g PE/ g Ti). Reference Examples 2 and 3 . Examples 2 and 3 are carried out as in Example 1 except using the catalyst amounts and reactor temperatures described in Table 1. The overall catalyst efficiencies are also shown in the Table. The polymer products of Examples 1-3 are tested for various structural, physical and mechanical properties and the results are given in Tables 2, 2A and 2B. Comparative Example A is Attane® 4001 polyethylene and comparative example B is Attane® 4003. Both comparative examples are made by The Dow Chemical Company and are commercial ethylene-octene copolymers produced under solution process conditions using a typical commercial Ziegler-type catalyst. The data show the polymers of the invention have more narrow molecular weight distributions (M w /M n ), higher melting points, better crystallization properties (i.e., higher crystallization onset temperatures) and, surprisingly, higher modulus than the commercial comparative examples A and B. The polymers of the invention surprisingly also show better optical properties (i.e., higher clarity and lower haze) than the comparative polymers, even though the polymers have about the same density. In addition, the polymers of the invention show better strength, toughness, tear and impact properties. Process Conditions for Reactor #1 for Examples 1-3 Ex. Monomer Volume (ml) Reactor #1 Temp. (°C) H 2 (Reactor #1) (mmol) Catalyst #1 (micromoles) 1 300 154 0 10 2 300 141 0 5 3 300 134 0 4 Process Conditions for Reactor #2 for Examples 1-3 Ex. Monomer Volume (ml) Reactor #2 Temp. (°C) H 2 (Reactor #2) (mmol) Catalyst #2 (micromoles) Overall Titanium Efficiency (g PE/g Ti) 1 300 185 100 6.4 344300 2 300 191 100 9 410100 3 300 193 100 9 425600 Examples 1-3 and Comparative Examples A and B Ex. Density (g/cm 3 ) Melt Index (I 2 ) (g/10 min) MFR (I 10 /I 2 ) M w M n MWD (M w /M n ) A 0.9136 1.06 8.33 122500 32500 3.77 B 0.9067 0.79 8.81 135300 31900 4.25 1 0.9112 1.07 7.4 115400 40000 2.89 2 0.9071 1.23 7.32 117600 40300 2.92 3 0.9062 1.08 7.46 124500 40100 3.1 Ex. Melting Temp. (°C) Crystl. Onset Temp. (°C) 2% Secant Modulus Young's Modulus (psi) Clarity (specular trans.) Haze (%) A 121 105 20389 20425 0.85 67 B 121 105 13535 13541 1.32 56 1 124 111 25634 25696 2.7 65 2 123 111 28144 28333 5.5 62 3 223 111 28650 28736 3.7 61 Ex. Yield Strength (psi) Yield Elongation (%) Break Strength (psi) Break Elongation (%) Toughness (ft.-lb.) Spencer Impact (psi) Tensile Strength (g/mil) A 1370 22 3133 693 1003 847 265 B 1108 24 2450 667 793 688 215 1 1541 16 4134 642 1155 897 311 2 1717 16 5070 658 1327 908 290 3 1756 15 4679 637 1234 903 311 Reference Example 4 Homogeneous Catalyst Preparation A known weight of the constrained-geometry organometallic complex [{(CH 3 ) 4 C 5 )}-(CH 3 ) 2 Si-N-(t-C 4 H 9 )]Ti(CH 3 ) 2 is dissolved in Isopar E to give a clear solution with a concentration of Ti of 0.001M. A similar solution of the activator complex, tris(perfluoropheny)borane (0.002M) is also prepared. A catalyst composition of a few mL total volume is prepared by adding 1.5 mL of Isopar E solution of Ti reagent. 1.5 mL of the borane (for B:Ti = 2:1) and 2 mL of a heptane solution of methylaluminoxane (obtained commercially from Texas Alkyls as MMAO Type 3A) containing 0.015 mmol Al to a 4 oz (100 ml) glass bottle. The solution is mixed for a few minutes and transferred by syringe to a catalyst injection cylinder on the polymerization reactor: Heterogeneous Catalyst Preparation A heterogeneous Ziegler-type catalyst is prepared similarly to that in Ex. 1 to give an active catalyst containing 0.009 mmol Ti and a final Al/Ti ratio of 8/1. This slurry is then transferred to a syringe in preparation for addition to the catalyst injection cylinder on the polymerization reactor. Polymerization A stirred, one-gallon (3.79L) autoclave reactor is charged with 2.1 L of Isopar™ E (made by Exxon Chemical) and 168 mL of 1-octene comonomer and the contents are heated to 120°C. The reactor is next charged with hydrogen and then with ethylene sufficient to bring the total pressure to 450 psig (3.2MPa). A solution containing 0.0015 mmol of the active organometallic catalyst described in the catalyst preparation section is injected into the reactor using a high pressure nitrogen sweep. The reactor temperature and pressure are maintained at the initial run conditions. After a 10 minute reaction time, the ethylene is shut off and the reactor is depressured to 100 psig (0.8MPa). At this time, an additional 168 mL of 1-octene is added to the reactor along with additional hydrogen and the contents heated. A slurry of the heterogeneous catalyst containing 0.009 mmol Ti prepared as described in the catalyst preparation section is injected into the reactor using a high pressure nitrogen sweep. The reactor is then continually fed ethylene at 450 psig (3.2MPa) and the reaction temperature quickly rises to 189°C where the polymerization is sustained for an additional 10 minutes. At this time the reactor is depressured and the hot polymer-containing solution transferred into a nitrogen-purged resin kettle containing 0.2 g Irganox™ 1010 (a hindered phenolic antioxidant made by Ciba Geigy Corp.) as a stabilizer. After removal of all the solvent in vacuo, the sample is then weighed (yield 202 g) to determine catalyst efficiencies (401630 g PE/ g Ti). Reference Examples 5-7 Examples 5-7 are carried out as in Example 4 except using the catalysts described in Example 1 and the catalyst amounts and reactor conditions described in Tables 3 and 3A. The overall catalyst efficiencies are also shown in Tables 3 and 3A. These examples show that the reaction conditions can be readily controlled to vary the composition and molecular weight distribution of the polymer through a simple change in catalyst amounts and monomer concentrations. Table 4 shows that the interpolymers produced in these examples have a broader molecular weight distribution than those of the earlier examples demonstrating a unique feature of the process control. The physical and mechanical properties still show surprising enhancements over typical commercial copolymers of comparable molecular weight and composition, particularly in strength, impact and tear properties. Comparing examples 4 and 5 with comparative example A (as well as by comparing examples 6 and 7 with comparative example B) shows that the crystallization properties of the polymers of the invention are largely unaffected by broadening the M w /M n . Process Conditions for Reactor #1 for Examples 4-7 Ex. Monomer Volume (ml) Reactor # 1 Temp. (°C) Reactor #1 H 2 Catalyst #1 (micromoles) Overall Titanium Efficiency (g PE/g Ti) 4 150+150 123 10 1.5 401630 5 150+150 139 50 5 422670 6 300+150 122 0 4 337241 7 300+150 133 100 6 434933 Process Conditions for Reactor #2 for Examples 4-7 Ex. Monomer Volume (ml) Reactor # 2 Temp. (°C) Reactor #2 H 2 (mmol) Catalyst #2 (micromoles) Overall Titanium Efficiency (g PE/g Ti) 4 150+150 189 300 9 401630 5 150+150 194 50 7.2 422670 6 300+150 189 400 9 337241 7 300+150 188 50 7.2 434933 Interpolymer Properties Ex. Density (g/cm 3 ) Melt Index (I 2 ) (g/10 min) MFR (I 10 /I 2 ) M w M n MWD (M w /M n ) A 0.9136 1.06 8.33 122500 32500 3.77 4 0.913 1.12 7.45 117900 29400 4.003 5 0.9136 1.17 8.07 135000 42100 3.209 B 0.9067 0.79 8.81 135300 31900 4.25 6 0.9108 3.3 7.4 89700 28700 3.122 7 0.9081 1.53 10.17 125700 31000 4.057 Ex. Melting peak (°C) Cryst. Onset Temp. (°C) Young's Modulus (psi) 2% Secant Modulus Clarity (specular trans.) Haze (%) A 121 105 20425 20389 0.85 67 4 123 110 20333 20292 4.7 72 5 123 110 22648 22609 2.32 72 B 121 105 13541 13535 1.32 56 6 124 112 20100 20074 1.15 72 7 123 112 19836 19800 1.85 67 Ex. Yield strength (psi) Yield elongation (%) Break strength (psi) Break elongation (%) Toughness (ft-lbs) Spencer Impact (psi) Tensile Tear (g/mil) A 1370 22 3133 693 1003 847 265 4 1468 19 3412 671 1012 977 271 5 1659 16 3608 738 1224 994 313 B 1108 24 2450 667 793 688 215 6 1354 16 2737 670 885 1022 255 7 1326 21 2353 729 914 821 238 Reference Example 8 Homogeneous Catalyst Preparation A known weight of the constrained-geometry organometallic complex ({(CH 3 ) 4 C 5 )}-(CH 3 ) 2 Si-N-(t-C 4 H 9 )]Ti(CH 3 ) 2 is dissolved in Isopar E to give a clear solution with a concentration of Ti of 0.001M. A similar solution of the activator complex, tris(perfluoropheny)borane (0.002M) is also prepared. A catalyst composition of a few mL total volume is prepared by adding 1.5 mL of Isopar E solution of Ti reagent, 1.5 mL of the borane (for B:Ti = 2:1) and 2 mL of a heptane solution of methylaluminoxane (obtained commercially from Texas Alkyls as MMAO) containing 0.015 mmol Al to a 4 oz (100 ml) glass bottle. The solution is mixed for a few minutes and transferred by syringe to a catalyst injection cylinder on the polymerization reactor. Heterogeneous Catalyst Preparation A heterogeneous Ziegler-type catalyst is prepared similarly to that in Ex. 1 to give an active catalyst containing 0.009 mmol Ti and a final Al/Ti ratio of 8/1. This slurry is then transferred to a syringe in preparation for addition to the catalyst injection cylinder on the polymerization reactor. Polymerization The polymerization described in this example demonstrates a process for the use of two catalysts, employed sequentially, in two polymerization reactors. A stirred, one-gallon (3.79L) autoclave reactor is charged with 2.1 L of Isopar™ E (made by Exxon Chemical) and 168 mL of 1-octene comonomer and the contents are heated to 120°C. The reactor is next charged with hydrogen and then with ethylene sufficient to bring the total pressure to 450 psig (3.2 MPa. A solution containing 0.0015 mmol of the active organometallic catalyst described in the catalyst preparation section is injected into the reactor using a high pressure nitrogen sweep. The reactor temperature and pressure are maintained at the initial run conditions. After a 10 minute reaction time, the ethylene is shut off and the reactor is depressured to 100 psig (0.8 MPa). At this time, an additional 168 mL of 1-octene is added to the reactor along with additional hydrogen and the contents heated. A slurry of the heterogeneous catalyst containing 0.009 mmol Ti prepared as described in the catalyst preparation section is injected into the reactor using a high pressure nitrogen sweep. The reactor is then continually fed ethylene at 450 psig (3.2MPa) and the reaction temperature quickly rises to 189°C where the polymerization is sustained for an additional 10 minutes. At this time the reactor is depressured and the hot polymer-containing solution transferred into a nitrogen-purged resin kettle containing 0.2 g Irganox™ 1010 (a hindered phenolic antioxidant made by Ciba Geigy Corp.) as a stabilizer. After removal of all the solvent in vacuo, the sample is then weighed (yield 202 g) to determine catalyst efficiencies (401630 g PE/ g Ti). Reference Examples 9-14 Examples 9-14 are carried out as in Example 8 except using the catalysts described in Example 1 and the catalyst amounts and reactor conditions described in Tables 5 and 5A. The overall catalyst efficiencies are also shown in the Tables. These examples show the ability to readily control the reaction conditions to vary the composition and molecular weight distribution of the polymer through a simple change in catalyst amounts and monomer concentrations. The polymers produced in these Examples show a broader molecular weight distribution than those of the earlier examples showing a unique feature of the process control. The physical and mechanical properties still show surprising enhancements over typical commercial copolymers of comparable molecular weight and composition, particularly in strength, impact and tear properties. Comparative Example C is Dowlex® 2045, a commercial ethylene/1-octene copolymer made by The Dow Chemical Company. Comparative Example D is Dowlex® 2047, a commercial LLDPE ethylene/1-octene copolymer made by The Dow Chemical Company. The data in Table 6 show that the molecular weight distribution (M w /M n ) can surprisingly remain relatively low, demonstrating a unique feature of the process control of the invention. Process Conditions for Reactor #1 for Examples 8-14 Ex. Monomer Volume (ml) Reactor #1 Temp (°C) Reactor #1 H 2 (mmol) Catalyst #1 (micromoles) Overall Titanium Efficiency (g PE/g Ti) 8 155 158 25 12.5 286100 9 155 146 20 7.5 312400 10 155 156 0 7.5 326600 11 205 155 0 10 311900 12 230 149 0 7.5 312400 13 155 152 0 7.5 305300 14 150+150 145 0 7.5 298200 Process Conditions for Reactor #2 for Examples 8-14 Ex. Monomer Volume (ml) Reactor #2 Temp (°C) Reactor #2 H 2 (mmol) Catalyst #2 (micromoles) Overall Titanium Efficiency (gPE/gTi) 8 155 190 150 7.2 286100 9 155 170 150 7.2 312400 10 155 188 200 7.2 326600 11 205 194 150 7.2 311900 12 230 194 150 7.2 312400 13 155 196 400 7.2 305300 14 150+150 195 150 7.2 298200 Ex. Density (g/cm 3 ) Melt index (I 2 ) (g/10 min) MFR (I 10 /I 2 ) M w M n MWD (M w /M n ) C 0.9202 1 ND 110000 27300 4.03 8 0.9257 3.1 6.72 80400 32000 2.5 9 0.9225 1.43 6.89 99400 36800 2.7 10 0.9234 1.57 7.04 100400 35200 2.85 D 0.9171 2.3 ND 85500 22000 3.89 11 0.9158 1.39 7.15 100000 35100 2.85 12 0.916 0.91 7.16 113200 37700 3 13 0.915 0.84 7.94 106900 33300 3.21 14 0.9186 1.09 7.1 106200 36400 2.9 ND = Not Determined Ex. Melt. Peak (°C) Crystal. Onset Temp. (°C) 2% Secant Modulus Young's Modulus (psi) Clarity (Specular Trans.) Haze (%) C ND 107 29169 29253 3.55 55 8 123 111 48123 48209 0.15 75 9 124 111 47815 47906 0.72 78 10 124 114 34077 34742 0.15 72 D ND ND 26094 26094 1.22 49 11 124 113 26245 26304 0.22 69 12 123 111 35492 35599 0.47 67 13 122 110 26466 26534 1.37 63 14 124 111 34989 35032 0.77 66 ND = Not Determined Ex. Yield Strength (psi) Yield elongation (%) Break strength (psi) Break elongation (%) Toughness (ft-lb) Spencer Impact (psi) Tensile Tear (g/mil) C 1830 13 4395 689 1292 735 316 8 2628 12 3893 620 1335 992 450 9 2403 13 4375 613 1343 753 367 10 2240 13 3619 600 1179 1043 326 D 1600 15 4061 771 1351 716 285 11 1905 15 5079 700 1480 820 334 12 2043 15 5385 610 1404 976 336 13 1818 21 4504 612 1203 977 247 14 1933 16 4755 653 1332 741 283 In step (B) of the Second Process, the ethylene and a-olefin materials may be present as unreacted materials in the reaction product from step (A) or they can each be added to the polymerization reaction mixture in step (B) as needed to make the desired interpolymer. In addition, hydrogen or other telogen can be added to the polymerization mixture of step (B) to control molecular weight. Reference Example 15 Example 15 is an in-situ blend made according to a continuous polymerization process. In particular, ethylene is fed into a first reactor at a rate of 52 lb/hr (24 kg/hr). Prior to introduction into the first reactor, the ethylene is combined with a diluent mixture comprising ISOPAR™ E hydrocarbon (available from Exxon) and 1-octene. With respect to the first reactor, the 1-octene:ethylene ratio is 9.6:1 (mole percent) and the diluent:ethylene ratio is 9.9:1 (weight). A homogenous constrained geometry catalyst and cocatalyst such as are described in Example 8 above and introduced into the first reactor. The catalyst and cocatalyst concentrations in the first reactor are 0.0030 and 0.0113 molar, respectively. The catalyst and cocatalyst flow rates into the first reactor are 0.537 lbs/hr (0.224 kg/hr) and 0.511 lbs/hr (0.232 kg/hr), respectively. The polymerization is conducted at a reaction temperature of 120°C. The polymer of the first reactor is an ethylene/1-octene copolymer and is estimated to have a density of 0.906 g/cm 3 , a melt flow ratio (I 10 /I 2 ) of about 8-10 and a molecular weight distribution (M w /M n ) of 2.2. The reaction product of the first reactor is transferred to a second reactor. The ethylene concentration in the exit stream from the first reactor is less than four percent, indicating the presence of long chain branching as described in U.S. Patent No. 5, 272,236. Ethylene is further fed into a second reactor at a rate of 58 lbs/hr (26 kg/hr). Prior to introduction into the second reactor, the ethylene and a stream of hydrogen are combined with a diluent mixture comprising ISOPAR™ E hydrocarbon (available from Exxon) and 1-octene. With respect to the second reactor, the 1-octene:ethylene ratio is 2.9:1 (mole percent), the diluent:ethylene ratio is 2.8 (weight), and the hydrogen:ethylene ratio is 0.106 (mole percent). A heterogeneous Ziegler catalyst and cocatalyst such as are described in Example 1 above are introduced into the second reactor. The catalyst and cocatalyst concentrations in the second reactor are 0.0023 and 0.0221 molar, respectively. The catalyst and cocatalyst flow rates into the second reactor are 1.4 lbs/hr (0.64 kg/hr) and 0.858 lbs/hr (0.39 kg/hr), respectively. The polymerization is conducted at a reaction temperature of 190°C. The polymer of the second reactor is an ethylene/1-octene copolymer and estimated to have a density of 0.944 g/cm 3 and a melt index (I 2 ) of 1.5 g/10 minutes. The total composition comprises 43 percent by weight of the polymer of the first reactor and 57 percent by weight of the polymer of the second reactor. The total composition has a melt index (I 2 ) of 0.53 g/10 minutes, a density of 0.9246 g/cm 3 , a melt flow ratio (I 10 /I 2 ) of 7.83, and a molecular weight distribution (M w /M n ) of 2.8.

Claims: A process for preparing an ethylene/α-olefin interpolymer composition, characterized by : (A) reacting by contacting ethylene and at least one other α-olefin under slurry or gas phase polymerisation conditions in the presence of a homogeneous catalyst composition in at least one reactor to produce a first interpolymer which has a narrow composition distribution, (i.e., one which has a composition distribution branch index (CDBI) of greater than 50 percent where CDBI is defined at the weight percentage of polymer molecules having a comonomer content within 50 percent of the median total comonomer content as measured by the TREF technique defined herein), and a narrow molecular weight distribution (i.e. a molecular weight distribution such that M w /M n is less than 3), wherein 15% or less of the first interpolymer has a degree of branching of less than or equal to 2 methyls/1000 carbons and is lacking a measurable homopolymer fraction as measured by the TREF technique, and wherein the homogeneous catalyst composition contains either no aluminum cocatalyst or contains an amount of aluminum cocatalyst which will give rise to a detectable aluminum residue in the product of less than or equal to 250 ppm, (B) reacting by contacting ethylene and at least one other α-olefin under slurry or gas phase polymerization conditions and at a higher polymerization reaction temperature than used in step (A) in the presence of a heterogeneous Ziegler catalyst in at least one other reactor to produce a second interpolymer which has a broad composition distribution (i.e. a composition distribution such that the composition has a homopolymer fraction as measured by the TREF technique and has multiple melting peaks), and a broad molecular weight distribution (i.e. a molecular weight distribution such that M w /M n is greater than 3), wherein 10 weight percent or more of the second interpolymer has a degree of branching of less than 2 methyls/1000 carbons, and wherein 25 weight percent or less of the second interpolymer has a degree of branching of 25 methyls/1000 carbons or more, wherein the Ziegler catalyst comprises (i) a solid support component derived from a magnesium halide or silica, and (ii) a transition metal component represented by the formula: TrX' 4-q (OR 1 ) q , TrX' 4-q (R 2 ) q , VOX'3 or VO(OR 1 ) 3 , wherein: TR is a Group, IVB, VB, or VIB metal, q is 0 or a number equal to or less than 4, X' is a halogen, and R 1 is an alkyl group, aryl group or cycloalkyl group having from 1 to 20 carbon atoms, and R 2 is an alkyl group, aryl group, aralkyl group, or substituted aralkyl group, and (C) combining the first interpolymer with the second interpolymer to form a polymer comprising the ethylene-α-olefin interpolymer composition, and (D) if necessary, removing the solvent from the polymer of step (C) and recovering the ethylene-α-olefin interpolymer composition. A process for preparing an ethylene/α-olefin interpolymer composition, characterized by : (A) polymerizing ethylene and at least one other α-olefin under slurry or gas phase polymerization conditions in at least one reactor containing a homogeneous catalyst composition to produce a first interpolymer which has a narrow composition distribution, (i.e., one which has a composition distribution branch index (CDBI) of greater than 50 percent where CDBI is defined at the weight percentage of polymer molecules having a comonomer content within 50 percent of the median total comonomer content as measured by the TREF technique defined herein), and a narrow molecular weight distribution (i.e. a molecular weight distribution such that M w /M n is less than 3), wherein 15% or less of the first interpolymer has a degree of branching of less than or equal to 2 methyls/1000 carbons and is lacking a measurable homopolymer fraction as measured by the TREF technique, and wherein the homogeneous catalyst composition contains either no aluminum cocatalyst or contains an amount of aluminum cocatalyst which will give rise to a detectable aluminum residue in the product of less than or equal to 250 ppm, (B) sequentially passing the interpolymer of (A) into at least one other reactor containing a heterogeneous Ziegler catalyst, ethylene and at least one other α-olefin, under slurry or gas phase polymerization conditions and at a higher polymerization reaction temperature than used in step (A) to produce an ethylene/α-olefin interpolymer composition, wherein the Ziegler catalyst comprises (i) a solid support component derived from a magnesium halide or silica, and (ii) a transition metal component represented by the formula: TrX' 4-q (OR 1 ) q , TrX' 4-q (R 2 ) q , VOX'3 or VO(OR 1 ) 3 , wherein: TR is a Group, IVB, VB, or VIB metal, q is 0 or a number equal to or less than 4, X' is a halogen, and R 1 is an alkyl group, aryl group or cycloalkyl group having from 1 to 20 carbon atoms, and R 2 is an alkyl group, aryl group, aralkyl group, or substituted aralkyl group, and (C) combining the first interpolymer with the second interpolymer to form a polymer comprising the ethylene-α-olefin interpolymer composition, and (D) if necessary removing the solvent from the polymer solution of step (C) and recovering the ethylene-α-olefin interpolymer composition. The process of any one of the preceding claims, wherein the α-olefin is 1-octene. The process of any one of the preceding claims, wherein the homogeneous catalyst composition comprises a metal co-ordination complex comprising a metal of group 4 of the Periodic Table of the Elements and a delocalised n-bonded moiety substituted with a constrain-inducing moiety, said complex having a constrained geometry about the metal atom such that the angle at the metal between the centroid of the delocalised, substituted n-bonded moiety and the centre of at least one remaining substituent is less than such angle in a similar complex containing a similar n-bonded moiety lacking in such constrain-inducing substituent, and provided further that for such complexes comprising more than one delocalised, substituted n-bonded moiety, only one thereof for each metal atom of the complex is a cyclic, delocalised, substituted n-bonded moiety. The process of any one of the preceding claims wherein the homogeneous catalyst composition further comprises an activating cocatalyst. The process of any one of Claims 1 to 5 wherein the homogeneous catalyst composition comprises a metal co-ordination complex corresponding to the formula: wherein: M is a metal of group 4 of the Periodic Table of the Elements; Cp* is a cyclopentadienyl or substituted cyclopentadienyl group bound in an η 5 bonding mode to M; Z is a moiety comprising boron, or a member of group 14 of the Periodic Table of the Elements, and optionally sulfur or oxygen, said moiety having up to 20 non-hydrogen atoms, and optionally Cp* and Z together form a fused ring system; X independently each occurrence is an anionic ligand group having up to 30 non-hydrogen atoms; n is 1 or 2; and Y is an anionic or nonanionic ligand group bonded to Z and M comprising nitrogen, phosphorus, oxygen or sulfur and having up to 20 non-hydrogen atoms, optionally Y and Z together form a fused ring system. The process of any one of Claims 1 to 5 wherein the homogeneous catalyst composition comprises a metal co-ordination complex corresponding to the formula: wherein: R' each occurrence is independently selected from the group consisting of hydrogen, alkyl, aryl, and silyl, and combinations thereof having up to 20 non-hydrogen atoms; X each occurrence independently is selected from the group consisting of hydride, halo, alkyl, aryl, silyl, aryloxy, alkoxy, amide, siloxy and combinations thereof having up to 20 non-hydrogen atoms; Y is -O-, -S-, -NR*-, -PR*-, or a neutral two electron donor ligand selected from the group consisting of OR*, SR*, NR* 2 or PR* 2 ; M is a metal of group 4 of the Periodic Table of the Elements; and Z is SiR* 2 , CR* 2 , SiR* 2 SiR* 2 , CR* 2 CR* 2 , CR*=CR*, CR* 2 SiR* 2 , BR*; wherein R* each occurrence is independently selected from the group consisting of hydrogen, alkyl, aryl, silyl, halogenated alkyl, halogenated aryl groups having up to 20 non-hydrogen atoms, and mixtures thereof, or two or more R* groups from Y, Z, or both Y and Z form a fused ring system; and n is 1 or 2. The process of any one of Claims 1 to 5 wherein the homogeneous catalyst composition comprises an amidosilane- or amidoalkanediyl- compound corresponding to the formula: wherein: M is titanium, zirconium or hafnium, bound in an η 5 bonding mode to the cyclopentadienyl group; R' each occurrence is independently selected from the group consisting of hydrogen, alkyl and aryl and combinations thereof having up to 7 carbon atoms, or silyl; E is silicon or carbon; X independently each occurrence is hydride, halo, alkyl, aryl, aryloxy or alkoxy of up to 10 carbons, or silyl; m is 1 or 2; and n is 1 or 2. The process of any one of Claims 1 to 5 wherein the homogeneous catalyst composition comprises an ionic catalyst having a limiting charge separated structure corresponding to the formula: wherein: M is a metal of group 4 of the Periodic Table of the Elements; Cp* is a cyclopentadienyl or substituted cyclopentadienyl group bound in an η 5 bonding mode to M; Z is a moiety comprising boron, or a member of group 14 of the Periodic Table of the Elements, and optionally sulfur or oxygen, said moiety having up to 20 non-hydrogen atoms, and optionally Cp* and Z together form a fused ring system; X independently each occurrence is an anionic ligand group having up to 30 non-hydrogen atoms; n is 1 or 2; and XA* - is - X(B(C 6 F 5 ) 3 ). The process of any one of the proceeding claims wherein the homogeneous catalyst composition has a reactivity ratio less than half that of the heterogeneous catalyst. An ethylene/α-olefin interpolymer composition producible by the process of any one of the preceding claims.

Inventors: CARDWELL ROBERT S, KOLTHAMMER BRIAN W S, CARDWELL, ROBERT S., KOLTHAMMER, BRIAN W.S.
Applicants: DOW GLOBAL TECHNOLOGIES INC, DOW GLOBAL TECHNOLOGIES INC.
Application year: 1994
Main classification: C08F297
IPC codes: C08L23, C08F297, C08F210, C08F4, C08F2